| Claims L Procedure destined to gases liquefaction which consists in using a gases liquefaction cycle, a cooling cascade and a power cycle, as for example Rankine, characterized in such that it is using a cascade of two coabsorbent refrigeration cycles for liquefaction cycle operation, which is coupling with a power cycle in condensation in such a way that an amount of the condensing heat of the power cycle is supplying with heat sotuve of low thermal level *°d free the two coabsorbent refrigeration cycles and the first cascade cycle, of quadruple truncated, type, is connected on one hand to the sink source of the power cycle, while on the other hand it is constituting the sink source of the cascade second cycle, of simple truncated type, in order that the latter is producing ultra- law temperature refrigaration, abbreviated by ULTR. 2. Procedure destined to H2 liquefaction, according to the 1st claim which consists in the simultaneous use of the procedure according to 1st claim and as well as in the use of an improved cycle of H2 liquefaction based on the synergy between the Joule-Thomson cycle, operated by the gas which must be liquefied and the Reverse Bryton cycle, operated by He, abbreviated next by J- T and RB, respectively, as well as on ULTR precooling processes and multi-stage compression with discharge gas superheat recovery processes applying on each stage the TWRC technology with Rankine Recovery Cyle-ULTR cooling, abbreviated next TWRC-RRC-ULTR, characterized in such that, the H2-evolution takes place, on one hand, in the J-T cycle, in several stages characterized by, • in the 1st stage, the J-T cycle is externally supplied by the subunit gas fraction „y* of H2, equal to that liquefied and then is ULTR precooled from the ambient temperature till the temperature obtained with the help of ULTR, •in the 2nd stage, the fraction „y”, coming of the 1st stage, is quasi-isothermal precooled with external supply of mechanical compression work input from a miniminn supposed pressure, sensibly equal to that ambient usually, till an intermediary higher and adequate value, but smaller as compared to that of the J-T expansion pressure, using a multi-stage precompression provided with TWRC-RRC-ULTR, • in the 3rd stage, the fraction coming of the 2nd stage, is subcooled in an isobar heat exchange in RB till a preestablished value, •in the 4th stage, the complementary gas fraction „1-y*’ of H2, resulted from the J-T expansion, is compressed from the liquefaction pressure, sensibly equal to the minimum one of H2 in the J-T cycle, till the said intermediary pressure, • in the 5th stage, the two complementary gas fractions and n1-y” of H2, coming of the 3rd and 4th stages, respectively, are mixed up in order to form the gas unit mass having the said intermediary pressure and an intermediary temperature of mixing, • in the 6th stage, the gas unit mass, coming of the 5th stage, is postcompressed from the said intermediary pressure and temperature till the adequate J-T expansion pressure and temperature, and •in the 7th stage, the gas unit mass, coming of the 6th stage, suffers the J-T expansion process till the liquefaction pressure and temperature, when the useful liquefied gas fraction „y” is produced, while, on the other hand, in the RB cycle, the gas He is sufering •first a mult-stage compression provided with TWRC-RRC-ULTR with external mechanical compression work input, from an adequate minimum pressure tin a maximum pressure, •then an adiabate expansion from the maximum pressure and a temperature sensible equal to that given by ULTR, till a pressure and temperature minimum, when external mechanical work output occurs, and •then an isobar heating process takes place through the heat exchange of RB from a minimum temperature till a temperature sensible equal to that given by ULTR, enabled by the subcooling of the fraction „y” of H2 from the J-T cycle, resulted from the 2nd stage, in order to close the cycle. 12 3. Procedure destined to industrial gases liquefaction, except H2, which here is considered for example for the He, consists in the simultaneous use of the procedure according to claim 1, as well as on the use of an improved gases liquefaction cycle based on the J-T and RB cycles synergy, as well as on ULTR precooling and TWRC-RRC-ULTR processes, characterized in such that the evolution of He, which is intended to be liquefied, takes place, on one hand, in the J-T cycle, in several stages, characterized by, • in the 1st stage, the J-T cycle is externally supplied by the subunit gas fraction „y” of He, equal to that liquefied and then is ULTR precooled from the ambient temperature till the temperature obtained with the help of ULTR, • in the 2nd stage, the complementaiy gas fraction „1-y” not liquefied, resulted from the J-T expansion, having the minimum pressure and temperature of liquefaction, is sufering a first recovery heating process, subcooling the gas unit which next is sufering the J-T expansion and then a second recovery heating process till a temperature sensibly equal to than given by the use of ULTR, subcooling an amount of the gas to be liquefied, found to the J-T expansion pressure, • in the 3rd stage, the fraction „y”, coming of the 1st stage, is mixing up with the fraction ,,1-y”, coming from the 2nd stage, in order to form a gas unit mass of pressure and temperature sensibly equal to the ambient value and that resulted from the use of the ULTR, respectively, • in the 4th stage, the gas unit mass, coming from the 3rd stage, is quasi-isothermal TWRC-RRC- ULTR multi-stage compressed till the J-T expansion pressure, with external mechanical compression work input, • in the 5th stage, the gas unit mass, coming of the 4th stage, is divided in two adequate complementary mass flow rates, • in the 6th stage, the first complementary gas mass flow cate, coming from the 5th stage, is recovery subcooled means the second recovery heating process of the complementary gas fraction ,,1-y”, mentioned in the 2nd stage, • in the 7th stage, the second complementary gas mass flow rate, coming of the 5th stage, is cooled in an isobar recovery heat exchange of RB, • in the 8th stage, the complementary mass flow rates, coming of the 5th stage, are mixed up after covering the 6th and the 7th stages, in order to rebuid the gas unit mass with the J-T expansion pressure and a temperature close to that resulted from the recovery isobar heat exchange process of RB, • in the 9th stage, the gass unit mass, coming of the 8th stage, is finally recovery subcooled in the first cooling enabled by the complementary gas fraction ,,1-y” of not liquefied gas, mentioned in the 2nd stage, and • in the 10th stage, the gas unit mass found to the adequate J-T expansion pressure and temperature, coming of the 9th stage, is expanded till the liquefaction pressure and temperature, when the useful liquefied gas fraction „y”, is produced, while, on the other hand, in the RB cycle, the gas He is sufering • first a quasi-isothermal TWRC-RRC-ULTR multi-stage compression from a minimum pressure till a maximum adequate pressure, with external mechanical compression work input, • then an adiabate expansion from the maximum pressure and a temperature sensibly equal to that given by ULTR till a minimum pressure and temperature, when external mechanical work output is provided, • and then a final isobar recovery heating process, enabled by the RB heat exchange from the minimum temperature till a temperature sensibly equal to that given by the ULTR, enabled by the cooling of the complementary mass flow rate of the gas unit mass of the J-T cycle, mentioned in the 7th stage, in order to close the cycle. . Procedure destined to industrial gases liquefaction, which consists in the use of one of the procedures according to claims 2 and 3 and in the generation of a superconductibility state in the electrical conductors of a gas liquefaction cycle, characterized in such that in a said gas liquefaction cycle a superconductibility state is selfinduced in its elements conducting electricity and belonging to the structure of electrical driving by achieving them out of adequate materials, such as for example out of Mb, in case of the He liquefaction, or out of Nb3Ge, in case of H2 liquefaction, and by cooling them permanently till temperatures T smaller than the critical temperatures of the said adequate materials, i.e. till T ≤ Tc,Nb = 8,31 K in cazul Nb and till T ≤ K,Nb3Ge — 22,4 K in case of Nb3Ge, using small amounts of the liquefied gas produced by the said gas liquefaction cycle, which eliminates completely the irreversible dissipative electrical losses caused by the Joule effect in these electrical conductors during said gas liquefaction plant operation. . Applying plant of the procedure, according to the claim 1, which is including generators, absorbers, resorbers, desorbers, preheaters, expanding valves, solution pumps, subcoolers, regulating valves, a condenser and a superheater, characterized in such that • an amount of the condenser (4) heat is transfered with the help of an intermediary heat transfer fluid, abbreviated by IHTF, to two closed circuits, made up by, • the first, out of the pipe (6), playing the role of secondary in the condenser (4), serially connected with the pipe (7), pump (8), 3-way valve (9), pipe (10), junction (11), pipe (12) and pipe (6), and • the second, out of the pipe (6), serially connected with the pipe (7), pump (8), the 3-way valve (9), pipe (13), junction (11), pipe (12) and pipe (6), in such a way that, on one hand, • the first circuit with ITHF supplies with heat source the generator (14) of a coabsorbent refrigeration plant quadruple truncated (15) by pipe (10), • the second circuit with ITHF supplies with heat source the generator of a second coabsorbent refrigeration plant simple truncated (17) by pipe (13), • the absorber (18) and resorber (19) of the plant (15) are cooled by the sink source (20) of the a SRC, • the plants (15) and (17) are thermally connected by desorber (21) of plant (15), which is sink source of the absorber (22) and of the resorber (23 ) of the plant (17), • their cooling is done by two closed circuits with IHTF with low freezing point, namely • the first closed circuit is made up of pipe (24) with role of secondary in the desorber (21), serially connected with pump (25), pipe (26), 3-way valve (27), pipe (28), jonction (29), pipe (24), while • the second out of the pipe (24), serially connected with pump (25), pipe (26), the 3-way valve (27), valve (28), pipe (30), jonction (29) and pipe (24), and, on the other hand, • the first circuit with ITHF with low freezing point is cooling the absorber (22) by pipe (28), • the second circuit is cooling the resorber (23) by pipe (30) and • the useful cooling effect ULTR is produced in the desorber (31) of the plant (17) and is accessed with the help of an IHTF with low freezing point (32). 6. Applying plant of the procedure, according to the claim 2, which is including, on one hand, generators, absorbers, resorbers, desorbers, preheaters, expanding valves, solution pumps, subcoolers, regulating valves, a condenser and a superheater, and, on the other hand, precoolers, multi-stage compressors with generators, condensers and recovery turbo-generators and a turbo- generator, characterized in such that, the H2 evolution takes place, on one hand, in the J-T cycle, in several stages, namely, • in the 1 st stage, a heat exchanger (33) is precooling the fraction „y” of H2 (34), of ambient pressure, externally supplied, with the help of a plant producing ULTR, indicated by IHTF (32), 14 • in the 2nd stage, the fraction „y”, precooled, coming of the 1st stage, is precompressed quasi- isothermal till an intermediary pressure with multi-stage compressors (35) and TWRC-RRC- ULTR, means IHTF (32), and becomes the fraction „y” (37), • in the 3rd stage, the fraction „y” (37) is, subcooled isobar in the heat exchanger (38) of RB and becomes the fraction „y” (39), • in the 4th stage, the gas fraction ,,1-y” of H2 (40), resulted from the J-T expansion, is precompressed quasi-isothermal, using external mechanical compression work, by a single-stage compressor (41) from the liquefaction pressure till the intermediary pressure and becomes the fraction „1-y” of H2 (42), • in the 5th stage, the two H2 complementary gas fractions „y” (39) si ,,1-y” (42), coming of the 3rd and 4th stages, are mixed up in order to form a gas unit mass (43) with the intermediary pressure and an intermediary mixing temperature, • in the 6th stage, the gas unit mass (43), is postcompressed by a single-stage compressor (44) from the intermediary pressure and temperature till the adequate J-T expansion pressure and temperature, and • in the 7th stage, the gas unit mass, generated in lhe 6th stage, is sufering the J-T expansion process till the liquefaction pressure and temperature, with the help of the expansion valve (45), when the useful liquefied gas fraction „y” (46) is produced, while, on the other hand, in the RB cycle the gas He is sufering • first a quasi-isothermal compression with multi-stage compressors (47) and TWRC-RRC-ULTR, means IHTF (32), • then an adiabate expansion in a turbo-generator (49) and finally, • an isobar heating process in a heat exchanger (50) enabled by the subcooling of the fraction „y” of H2 (37) of the J-T circuit, in order to close the cycle. 7. Applying plant of the procedure, according to claim 3, which is including, on one hand, generators, absorbers, resorbers, desorbers, preheaters, expanding valves, solution pumps, subcoolers, regulating valves, a condenser and a superheater, and, on the other hand, precoolers, multi-stage compressors with; generators, condensers and recovery turbo-generators and a turbo- generator, characterized in such that the evolution of the gas to be liquefied, here for example He, takes place on one hand in the J-T cycle in several stages, namely, • in the 1st stage, a heat exchanger (51) is precooling the gas fraction ,,y” (52), of ambient pressure, externally supplied, with the help of an ULTR plant, indicated by IHTF (32), • in the 2nd stage, the gas fraction ,,1-y” (53), resulted from the J-T expansion, is sufering a first recovery heating process in a heat exchanger (54), subcooling the gas unit mass which is sufering next the J-T expansion and then a second recovery heating process in a second heat exchanger (55), subcooling an amount of the gas to be liquefied, found to the J-T expansion pressure, • in the 3rd stage, the subcooled gas fractions „y” (52) and ,,1-y” (53), coming of the 1st and 2nd stages, respectively, are mixed up in order to form the subcooled gas unit mass (56) subsequently partially liquefied, • in the 4th stage, the gas unit mass (56) is compressed quasi-isothermal till the J-T expnsion pressure, with the help of multi-stage compressors (57) and TWRC-RRC-ULTR, means IHTF (32), • in the 5th stage, the gas unit mass, from the 3rd stage, is divided in two complementary fractions (59) and (60) with the help of a 3-way valve (61), • in the 6th stage, the complementary fraction (59) is recovery subcooled by the second heating process of the complementary fraction ,,1-y” (53), in the heat exchanger (55), • in the 7th stage, the complementary fraction (60) is cooled in the recovery heat exchanger (62) of RB, 15 • in the 8th stage, the complementary fractions (59) and (60) are mixed up together, after being precooled, in order to form the gas unit mass (63) with the J-T expansion pressure and a temperature close to that resulted from the recovery isoter heat exchange of RB, • in the 9th stage, the gas unit mass, coming from the 8th stage, is finally subcooled in the recovery heat exchanger (54), and • in the 10th stage, the gas unit mass coming from the 9th stage, is expanded from the J-T pressure and temperature till the liquefaction pressure and temperature, with the help of the expansion valve (64), in order to produce the useful liquefied gas fraction „y” (65), while, on the other hand, in the RB cycle, the gas He is suffering first • a quasi -isothermal compression with the help of multi-stage compressors (66) with TWRC-RRC- ULTR, means IHTF (32), then it is suffering • an adiatete expansion in a turbo-generator (68) till to a minimum pressure and temperature and then, • an isobar heating process in the heat exchanger (69) with the help of die complementary fraction (60) cooling, in order to close the cycle. 8. Applying plant of the procedure, according to claim 4, which is including, on one hand, generators, absorbers, resorbers, desorbers, preheaters, expanding valves, pumps of solution, subcoolers, regulating valves of mass flow rate, a condenser, a turbo-generator and a superheater, and, on the other hand, precoolers, multi-stage compressors with generators, condensers and recovery turbo-generators and a turbo-generator, as well as heat exchangers and statoric and rotoric wireing af the electrical driving of the compressors, pumps and other electrical power consumers, characterized in such that, the useful liquefied gas fraction „y” (70), achieved by the plant, is divided in two complementary parts playing different role, namely, • the first (1 — k)y (71), is employed for external use and • the second ky (72), is used to selfinduce a superconductibility state in the electrical conductors elements of own structure of electrical driving, where 0 < k « 1, 0 < y < 1, ky « 1, achieved in such a way that •the motors statoric and rotoric wireing playing the role of electrical driving of the compressors, pumps and other electrical consumers, generically noted by (73-1), (73-2), ..., (73-(n-l)), (73-n), are made up of adequate materials, chosen in such a way that the temperature of gas liquefaction, achieved by the liquefaction plant, be capable to ensure their continuous coolings below their superconductibility critical temperature, with the help of some heat exchangers, generically noted by (74-1), (74-2), (74-(n-l)), (74-n), n G N, of a pump (75) circulating the fraction ky (72) and of a hydrolic circuit made up Of two collectors (76) and of pipes connected in parallel (77) between the collectors (76), provided each with regulating valves (78), so that, • as a consequence of the cooling below critical temperatue, the said wireing to become electrical superconductor, • the liquid fraction ky (72) to become gas fraction (79), • and the gas fraction (79) to be mixed up with the complementary gas fraction (1 - k)y (80), introduced externally in the liquefaction plant to form the gas mass fractions y (81), in order to start a new cycle of gas liquefaction provided with selfinduction of superconductibility in its electrical conductors during operation. 16 |
This invention is referring to a gas liquefaction procedure and to an applying plant thereof, which are transported and utilized further in an effective way in industrial, agricol, research, or household, etc., applications.
There are known a procedure and an applying plant, based on the SCC-HC/CBS-RB & J-T cycle. This cycle is using the synergic coupling of the known cycles Reverse Brayton and Joule-Thomson, abbreviated further by RB and J-T, respectively, and have been proposed to liquefy heluim (He), hydrogen (H 2 ), and methane (CH 4 ). In the mentioned cycle, RB is operated by He, and J-T by the gas which is desired to be liquefied. The main indicator of SCC-HC/CBS-RB & J-T is the specific mechanical work of compression, consumed for liquefaction, noted by l spec [kWhe*kg' 1 liquefied gas]. A measure to increase the indicator l spec , but sometimes also necessary for liquefaction achievement, is the precooling of the gas to be liquefied prior compression. Besides this, SCC-HC/CBS-RB & J-T is using processes of Thermal-to-Work Recovery Compression, abbreviated TWRC, or Thermal-to- Thermal Recovery Compression, abbreviated TTRC, but skipped here. These processes recover a part of the superheating of the compressed gases in an adiabatic way and is transforming it in useful mechanical work, delivered externally, or in useful cooling effect, in order to reduce the mechanical work consumed for the compression of a gas. These processes are applied to each compression stage of a multi-stage mechanical vapor compression process during of which a cooling of the condenser of a Rankine Recovery Cycle, abbreviated by RRC, of TWRC, takes place, and as well a completion of the compressed gas cooling between each stage. The cooling processes of 1he RRC condenser between compression stages take place below ambient temperature, e.g. T Mc = 288.15K, and is named generically Subambient Cooling Compression, abbreviated SCC, The processes of precooling and cooling mentioned are achieved by using the Ultra-Low Temperature Refrigeration, abbreviated by ULTR, obtained, e.g. at T D1 = 198.15K, with the help of the Coabsorbent Technology, abbreviated by CBS. This technology is employing the absorption refrigeration technology, characterized by a very small consumption of mechanical work, just for solution pumping. For example, each CBS unit can have a COP CBS = 150 — 300 It is supplied by low-temperature heat sources, which is desired to be free, e.g. T Mh = (308.15 — 313.15)K. In the text of the present invention, the reference to ULTR use covers all situations when it is used alone, or in the precooling processes and completion of cooling between compression stages of a stage-compression, as well as of ULTR for RRC in the TWRC processes applied to each stage of a stage-compresssion, noted farther by RRC-ULTR.
Due to the improvements of principle and technical, which SCC-HC/CBS-RB & J-T brings, its effectiveness is considerably higher as compared to that of the already existing cycles of gas liquefaction. However, despite this, the SCC-HC/CBS-RB & J-T cycle may benefit further of important improvements. These are constituting the technical problem which this invention is confronted with, presented next as four objectives. These objectives have as scope the elimination of some defficiencies which SCC-HC/CBS-RB & J-T are still confronted with.
A 1st objective of the present invention is to find a procedure and an applying plant as a technical solution capable to ensure an efficient operation of SCC-HC/CBS-RB & J-T with the help of ULTR during the whole year and in all industrial regions of the globe, using a free, low-temperature heat source, for CBS operation.
A 2nd objective of the present invention, achieved together with the 1st objective, is to find a procedure and an applying plant as a technical solution of SCC-HC/CBS-RB & J-T efficiency increase with the help of ULTR for liquefaction of hydrogen and similar gases, named further H 2 - SCC-CBS-RB & J-T. A 3rd objective of the present invention, achieved together with the 1st objective is to find a procedure and an applying plant as a technical solution of SCC-HC/CBS-RB & KT efficiency increase with the help of ULTR for liquefaction of gases, such as helium (He), neon (Ne), nitrogen (N 2 ), oxygen (O 2 ), argon (Ar), air, natural gas (NG), which do not belong to the calhegory of gases mentioned to the 2nd objective of invention and are named further He-SCC-CBS-RB & J-T.
A 4th objective of the present invention is to find a procedure arid an applying plant as a technical solution of increasing in a supplementary way the efficiency of the SCC-HC/CBS-RB & J-T cycle with the help of ULTR in case this has prior benefited of the simultaneous achievement of the 2nd or 3rd objective.
The procedure solves the technical problem, according to invention and 1st objective, in that H 2 - and- He-SCC-CBS-RB & J-T use a CBS cascade which is coupling with a steam power cycle, such as Rankine, operated in condensation, abbreviated by SRC, so that a part of the SRC condensing heat, of low-temperature and free, is supplying the CBS cascade as heat source and this is producing ULTR whole year, by the connection of SRC to the sink source.
The procedure is solving the technical problem, according to invention and 2nd objective, in that, on one hand, the H2 evolution in the J-T cycle takes place in several stages, namely
• in the 1st stage, the subunit gas fraction „y” of H 2 , which supplies externally the J-T cycle, equal to the liquefied fraction, is precooled from the ambient temperature, till the temperature obtained with the help of ULTR,
• in the 2nd stage, the fraction „y”, coming of the 1st stage, is precompressed quasi-isothermal using external mechanical work from a supply value, supposed to be minimum, sensibly equal to that of the ambient, to a higher value, intermediary and adequate, but smaller as compared to that of J-T expansion, in several stages provided each with TWRC and RRC-ULTR,
• in the 3rd stage, the fraction „y”, coming of the 2nd stage is subcooled in an isobar heat exchange in RB till a preestablished state,
• in the 4th stage, the complementary gas fraction ,,1-y” of H 2 , resulted from the J-T expansion, is compressed from the liquefaction pressure, sensible equal to that minimum of H 2 in the J-T cycle, till the intermediary pressure,
• in the 5th stage, the two comlementary gas fractions „y” and „l-y” of H 2 , coming of stages 3rd and 4th, respectively, are mixed up in order to form the unit mass of gas, having the intermediary pressure and an intermediary temperature of mixing,
• in the 6th stage, the unit mass of gas, coming of the 5th stage, is postcompressed from the intermediary pressure and temperature till the adequate pressure and temperature of J-T expansion,
• in the 7th stage, the unit mass of gas, coming of the 6th stage, is sufering the J-T expansion process till the pressure and temperature of liquefaction, when the useful liquefied gas fraction „y” of lb is produced, and, on the other hand, in the RB cycle, reprezented in a triangular way in the p-v diagram, the gas He suffers
• first a quasi-isothermal compression in several stages, each provided with TWRC and RRC- ULTR, with external mechanical work input, from a minimum pressure to a maximum adequate pressure,
• then, an adiabate expansion from the maximum pressure and a temperature sensibly equal to that gi ven by ULTR, till an adequate pressure and temperature of minimum values, when mechanical work is delivered externally and
• then an isobar heating through RB heat exchange from the minimum temperature till the temperature sensibly equal to that given by ULTR, enabled by the subcooling of the gas fraction „y” of H 2 of the J-T cycle, resulted from the 2nd stage, in order to close the cycle. The procedure solves the technical problem, according to present invention and to the 3rd objective in that, on one hand, in the J-T cycle the evolution of the gas which must liquefied takes place in several stages, namely,
• in the 1st stage, the subunit gas fraction „y”, which is supplying the J-T cycle externally with the gas which must be liquefied, having the pressure and temperature sensibly equal to those of the ambient and a mass equal to that to be liquefied, is precooled till the temperature obtained with the help of ULTR,
• in the 2nd stage, the complementary gas fraction ,,1-y” of not liquefied gas, resulted from the J-T expansion, having the minimum pressure and temperature of liquefaction, is sufering a first recovery heating process, by subcoolig the unit mass of gas which subsequently is sufering the J- T expansion and then is sufering a second recovery heating process, till a temperature sensibly equal to that given by ULTR, by subcooling a part of the gas to be liquefied, of pressure equal to that of J-T expansion,
• in the 3rd stage, the fraction „y”, coming of the 1st stage, is mixed up with the fraction ,,1-y”, coming from the 2nd stage, in order to form the unit mass of gas, of pressure and temperature sensible equal to that of ambient and to that resulted from the use of ULTR, respectively,
• in the 4th stage, the unit mass of gas, coming of the 3rd stage, is compressed quasi-isothermal with the help of external mechanical work input; in several stages provided each by TWRC and RRC- ULTR, till the J-T expansion pressure,
• in the 5th stage, the unit mass of gas, coming of the 4th stage, is divided in two adequate complementary mass flow rates,
• in the 6th stage, the first complementary gas part, coming of the 5th stage, is recovery subcooled with the help of the second heating recovery process of the complementary fraction ,,1-y”, mentioned in the 2nd stage,
• in the 7th stage, the second complementary gas fraction, coming of the 5th stage, is recovery subcooled by an isobar heat exchange in RB,
• in the 8th stage, the complementary fractions, coming of the 5th stage, are mixed up after covering the 6th and 7th stages, in order to rebuild the unit mass of gas having the pressure of the J-T expansion and the temperature close to that resulted from the RB recovery isobar heat exchange,
• in the 9th stage, the unit mass of gas coming of the 8th stage, is subcooled finally by the first recoveiy heat exchange taking place with the complementary gas fraction ,,1-y” of not liquefied gas, mentioned in the 2nd stage, and
• in the 10th stage, the unit mass of gas, found to the adequate pressure and temperature of the J-T expansion, coming of the 9th stage, is expanded till the pressure and temperature of liquefaction, when the useful fraction of liquefied gas is produced, and, on the other hand, in the RB cycle, represented in a tringular way in the diagram p-v, the He gas is sufering
• first a quasi-isothermal compression done with the help of external mechanical work input, taking place with several compression stages, each provided with TWRC and RRC-ULTR, from a minimum pressure till a maximum adequate value,
• then, an adiabate expansion from the maximum pressure and a temperature sensibly equal to that given by ULTR till a minimum adequate pressure and temperature, when mechanical work is produced and externally delivered,
• then an isobar heating process takes place by a recovery heat exchange of RB from the minimum temperature till that given by the ULTR, enabled by the cooling of complementary gas fraction of the unit mass of gas of the J-T cycle, mentioned in the 7th stage, in order to close the cycle.
The procedure solves the technical problem, according to the present invention and to the 4th objective, in that the elements conducting electricity, which build up the structure of the electrical driving systems of H 2 - and-He-SCC-CBS-RB & J-T, are made up of adequate materials, which are continuously cooled by a small fraction of the gas liquefied by H 2 - and-He-SCC-CBS-RB & J-T, so that this becomes electrical superconductor and m this way it is eliminating completely the electrical losses caused by the irreversible thermal dissipation caused by Joule effect taking place in theirs electrical conductors during theirs operation.
The applying plant, according to the 1st objective of the invention, is using for example a cascade of two plants of cooling truncated CBS type, which are coupled with a power plant of SRC type, in such a way that on one hand a part of the SRC condensing heat plays the role of heat source of the cascade generators, the resorption and absorption heats of the cascade are eliminated with the help of the SRC sink source and of one of the cascade desorbers, while, on the other hand, the second cascade desorber is producing the useful effect of ULTR.
The applying plant, according to 2nd objective of invention, uses on one hand in the J-T cycle
• in the 1st stage, a heat exchanger to ensure ah ULTR precooling of the gas fraction „y” of H 2 , externally supplied,
• in the 2nd stage, the fraction coming of the 1st stage, is precompressed quasi-isothermal till an intermediary pressure using stage-compression provided to each stage with TWRC and RRC- ULTR,
• in the 3rd stage, the fraction „y”, coming of the 2nd stage, is isobar precooled in the RB heat exchange process,
• in the 4th stage, the fraction „l-y” of H 2 , resulted from the J-T expansion, is adiabatical precompressed with the help of external mechanical work by a single-stage compressor from the liquefaction pressure till the intermediary pressure,
• in the 5th stage, the two complementary gas fractions „y” and ,,1-y”, coming of the 3rd and 4th stages, respectively, are mixed up in order to form the unit mass of gas having the intermediary pressure and an intermediary temperature of mixing,
• in the 6th stage, the unit mass of gas, generated in the 5th stage, is postcompressed by a single- stage compressor from the intermediary pressure and temperature to the adequate pressure and temperature of J-T expansion, and
• in the 7th stage, the unit mass of gas, generated in the 6th stage, is sufering the J-T expansion process till the liquefaction pressure and temperature, when the useful liquefied gas fraction „y” is produced, and, on the other hand, in the RB cycle, the He gas is sufering
• first a quasi-isothermal compression with several stages, each provided with TWRC and RRC- ULTR and external mechanical work input,
• then an adiabate expansion in a turbo-generator, with external useful work delivery, and
• finally, an isobar heating process in a heat exchanger, enabled by subcooling the gas fraction ,.y” of H 2 from the J-T cycle, in order to close the cycle.
Applying plant, according to the 3rd objective of invention, uses on one hand in the J-T cycle
• in the 1 st stage, a CBS plant which produces ULTR in order to precool the gas fraction „y” of the gas to be liquefied, externally supplied,
• in the 2nd stage, the fraction ,,1-y”, resulted from the J-T expansion, is sufering a first recovery heating process in a heat exchanger, subcooling the unit mass of gas which subsequently is sufering the J-T expansion, then, a second heating process, in a second heat exchanger, subcooling a part of the gas having the pressure of J-T expansion,
• in the 3rd stage, the gas fractions „y” and ,,1-y”, coming of the 1st and 2nd stage, respectively, are mixing up in order to form the unit mass of gas,
• in the 4th stage, the unit mass of gas, coming of the 3rd stage, is quasi-isothermal compressed in several stages till the J-T expansion pressure, with the help of multi-stage compressors and each stage is provided with TWRC and RRC-ULTR, • in the 5th stage, the unit mass of gas of H 2 is divided in two complementary mass flow rates.
• in the 6th stage, the first complementary part of the unit mass of gas is recovery subcooled by a second recovery heating process of the complementary gas fraction ,,1-y”, in the second heat exchanger mentioned in the 2nd stage,
• in the 7th stage, the second complementary fraction of the unit mass of gas of H 2 , mentioned in the 5th stage and having the J-T expansion pressure, is isobar cooled in the RB recovery heat exchanger,
• in the 8th stage, the complementary fractions which have covered the 6th and 7th stages, are mixed up in order to rebuild the unit mass of gas of H 2 , having the J-T expansion pressure and a temperature close to that resulted from the isobar recovery heat exchange in RB heat exchanger,
• in the 9th stage, the unit mass of gas coming of the 8th stage is subcooled finally in the first recovery heat exchanger, mentioned in the 2nd stage, with the help of the complementary gas fraction „l-y” of H 2 not liquefied, and
• in the 10th stage, the unit mass of gas coming of the 9th stage, is J-T expanded by an expansion valve from the J-T expansion pressure and temperature till the liquefaction pressure and temperature, when the useful H 2 liquefied gas „y” fraction is produced, and, on the other hand, in the RB cycle, the He gas is sufering
• first a quasi-isothermal compression done with multi-stage compressors, provided with TWRC and RRC-ULTR in each stage,
• then an adiabate expansion in a turbo-generator, with external useful work delivery, till a minimum pressure and temperature and,
• then an isobar heating process in a heat exchanger, when the complementary fraction of the unit mass of H 2 gas, mentioned in the 7th stage, is cooled, in order to close the cycle.
The applying plant, according to the 4th objective of the invention, uses in the structure of the driving electrical motors of H 2 - and-He-SCC-CBS-RB & J-T electrical conductors made up of adequate materials, which are permanently cooled by a small amount of the liquefied gas obtained by SCC- CBS-RB & J-T, in such a way that these are becoming electrical superconductors and H 2 - and-He- SCC-CBS-RB & J-T are capable to eliminate completely the electrical losses in theirs electrical conductors, caused by the thermal irreversible electrical dissipation, i.e. by Joule effect, during theirs operation.
The advantages offered by the invention are the followings:
- The technical solution ensures effective operation of the H 2 - and-He-SCC-CBS-RB & J-T cycles due to ULTR use the whole year and in all industrial zones of the globe;
- The technical solution ensures the increase of H 2 - and-He-SCC-CBS-RB & J-T cycles efficiency with the help of ULTR employed in the liquefaction of all important and known technical gases;
- The technical solution ensures additional H 2 - and-He-SCC-CBS-RB & J-T cycles efficiency increase with the help of ULTR in case this is setfinducing an electrical superconductibility state in its electrical conductors used in the electrical driving.
Next, an example of invention achieving is done as well in relation to Figs. 1-9:
- Fig. 1. Flow-chart of CBS cascade and SRC coupling for ULTR production;
- Fig. 2. H 2 -SCC-CBS-RB & J-T gas liquefaction plant flow-chart for H 2 and similar gases;
- Fig. 3. Plot of some parameters of H 2 -SCC-CBS-RB & J-T gas liquefaction plant vs. J-T expansion pressure;
- Fig. 4. Plot of He-H 2 isobar heat exchange vs. fluid temperatures in RB; - Fig. 5. He-SCC-CBS-RB & J-T gas liquefaction plant flow-chart for He and other similar gases;
- Fig. 6. A 1st plot of some parameters of He-SCC-CBS-RB & J-T gas liquefaction plant for He and similar gases vs. J-T expansion pressure;
- Fig. 7. A 2nd plot of some parameters of He-SCC-CBS-RB & J-T gas liquefaction plant for He and similar gases vs. J-T expansion pressure;
- Fig. 8. Simplified flow-chart of H 2 - and-He-SCC-CBS-RB & J-T gas liquefaction plants benefiting of selfinduction of electrical superconductibility of its driving motors electrical conductors;
- Fig. 9. Plot of specific work consumed by SCC-CBS-RB & J-T gas liquefaction plant for He, benefiting of selfinduction of electrical superconductibility of its driving motors electrical conductors in function of the ratio length / section area of superconductor;
- Fig. 10. Plot of specific work consumed by SCC-CBS-RB & J-T gps liquefaction plant for H2, benefiting of selfinduction of electricarsupeitonductibility of its driving motors electrical conductors in function of the ratio length / section area of superconductor;
The achievement procedure, according to invention, is using in the example of Fig. 1 a cascade of two CBS refrigeration cycles for H 2 - and-He-SCC-CBS-RB & J-T operation, which is coupled with a SRC Rankine cycle operating in condensation in such a way that a part of SRC condensation heat supplies with heat source of low-temperature and free, e.g. at T Mh , the two CBS refrigeration cycles and the 1st CBS cascade cycle, of cvadruple truncated type, is connected, On one hand, to the SRC sink source, and, on the other hand, is constituted in sink source of the 2nd CBS cascade cycle, of simple truncated type, in order that the latter is producing ULTR, e.g. at T or .
The applying plant, given in the achievement example of Fig, 1, according to invention, is using the thermal coupling with a power SRC plant for H 2 - and-He-SCC-CBS-RB & J-T operation. It is represented in a simplified way in the T-s diagram and is including a generator 1 , a vapor superheater 2, a turbo-generator 3, a condenser 4 and a pump 5. A part of the condenser 4 heat is transfered with the help of an intermediary heat transfer fluid, abbreviated by IHTF, and two closed circuits. The first closed circuit is made up by pipe 6, plying the role of secondary in the condenser 4, pipe 7, pump 8, the three-way valve 9, pipe 10, junction 11, pipe 12 and pipe 6, and the second circuit is made up by the pipe 6, pipe7, pump 8, the three-way valve 9, pipe 13, junction 11, pipe 12 and pipe 6. The 1 st circuit covered by ITHF supplies with heat source the generator 14 of a coabsorbent cvadruple truncated refrigeration plant 15 by means of pipe 10. The 2nd.circuit covered by ITHF supplies with heat source the generator of the second CBS cycle, i.e. a coabsorbent simple truncated refrigeration plant 17, by means of pipe 13. Both Coabsorbent truncated refrigeration plants are represented is a symbolic way in the log p - (-1/T) diagram, according to (Staicovici, 2014). The absorber 18 and resorber 19 of the plant 15 are cooled by the sink source 20 of SRC. The plants 15 and 17 are connected in the thermal cascade by the desorber 21 of the plant 15, which is the cooling source of the absorber 22 and resorber 23 of the plant 17. Their cooling is done by two closed circuits covered by a ITHF with low freezing point The 1st closed circuit is made up of the pipe 24, playing the role of secondary in the desorber 21, pump 25, pipe 26, the three-way valve 27, pipe 28, with role of secondary in the absorber 22, jonction 29, pipe 24, and the 2nd closed circuit is made up of pipe 24, pump 25, pipe 26, the three-way valve 27, pipe 30, with role of secondary in the resorber 23, junction 29 and pipe 24. The useful ULTR is produced by the desorber31 of plant 17 and is accessed with the help of an ITHF with low freezing point 32.
The achieving procedure, according to invention, is describing in example of Fig. 2 the evolution of H 2 in the J-T cycle, on one hand, in several stages, namely, • in the 1 st stage, the subunit gas fraction „y” of H 2 , e.g. y = 0.81kg/kg, which supplies externally the J-T cycle, equal to the liquefied fraction, is preceded from the ambient temperature, e.g. T Mh = 288.15 K, till the temperature achieved by ULTR, e.g. T D! — 198.15K.
• in the 2nd stage, the fraction „y”, coming from the 1st stage, is precompressed quasi-isothermal with external mechanical work input from a supply value, supposed minimum, usually sensible equal to the ambient pressure, e.g. p = Ibar, till a higher value, intermadiary, adequate, e.g. p = 3 bar, but smaller as compared to the J-T expansion pressure, e.g. p =s 4.85 bar, in several stages, each provided with TWRC and RRC-ULTR,
• in the 3rd stage, the fraction „y”, coming from the 2nd stage, is subcooled in an isobar heat exchange in RB till a value preestablished, e.g. T = 20.4K,
• in the 4th stage, the complementary gas fraction ,,1-y” of H 2 , rezuled from the J-T expansion, is compressed from the liquefaction pressure, sensibly equal to the minimum pressure of H 2 in J-T cycle, e.g. p = Ibar, till the intermediary pressure, e.g. p = 3bar,
• in the 5th stage, the two complementary gas fractions „y” and ,,1-y” of H 2 , coming from the 3rd and 4th stages, respectively, are mixed up in order to form a unit mass of gas, m = 1kg /kg having the intermediary pressure and a mixing up temperature, e.g. p = 3bar, T = 21K,
• in the 6th stage, the unit mass, coming from the 5th stage, is postcompressed from the intermediary pressure and temperature till the adequate pressure and temperature of J-T expansion, e.g. p - 4.85bar,T S28K, and
• in the 7th stage, the unit mass of gas, coming from the 6th stage, is sufering the J-T expansion process till the pressure and temperature of liquefaction, e.g. p = Ibar.T S20.4K, when the useful liquefied gas fraction „y” is produced, e.g. y = 0.81 kg /kg, and, on the other hand, in the RB cycle the He gas is sufering
• first a quasi-isothermal compression in several stages, each provided with TWRC, RRC-ULTR, and external mechanical work input, e.g. w » 2650 k]/kg, from an adequate minimum pressure, e.g. p = 0.1 bar, till a maximum pressure, e.g. p s 42 bar,
• then an adiabate expansion from the maximum pressure and a temperature sensibly equal to that given by ULTR, e.g. T Dt ~ 198.15/C, till a minimum adequate pressure and temperature, e.g. p = O.lbar, T = 18.4K, provided with external mechanical work output, e.g. w « 850 kJ /kg, and
• then an isobare heating process ensured by the RB heat exchange from the minimum temperature, e.g. T — 18.4K, to a temperature sensibly equal to that given by ULTR, e.g. T DI = 198.15K, enabled by the subcooling of the gas fraction „y” of H 2 of the J-T cycle, resulted from the 2nd stage, e.g. T = 200.15K to T = 20.4/f, in order to close the cycle.
The applying plant, according to invention, given in the example of achievement ofFig.2, is ensuring, on one hand, the H 2 evolution in the J-T cycle in several stages, namely,
• in the 1 st stage, a heat exchanger 33 is precooling the fraction „y” of H 2 34, of ambient pressure, externally supplied, with the help of an ULTR plant, indicated by IHTF 32, only,
• in the 2nd stage, the precooled fraction „y”, coming of the 1st stage, is precompressed quasi- isothermal till an intermediary pressure with multi-stage compressors 35, and stages provided each with TWRC and RRC-ULTR 36, so that it becomes fraction „y” 37,
• in the 3rd stage, fraction „y” 37 is isobar subcooled in the heat exchanger 38 of RB and becomes fraction „y” 39,
• in the 4th stage, Ute gas fraction ,,1-y” of H 2 40, resulted from the J-T expansion, is precompressed quasi-isothermal with external mechanical work input, by a single-stage compessor 41, from the liquefaction pressure till the intermediary pressure and becomes fraction „1-y” 42,
• in the 5th stage, the two complementary gas fractions „y” 39 and „1-y” 42, coming from stages 3rd and 4th, respectively, are mixing up in order to form a unit mass of gas 43, with intermediary pressure and intermadiary temperature of mixing, • in the 6th stage, the unit mass of gas 43 is postcompressed by a single-stage compressor 44, from the intermediary pressure and temperature till adequate temperature and pressure of J-T expansion and
• in the 7th stage, the unit mass of gas, generated in the 6th stage, is sufering the J-T expansion till the liquefaction pressure and temperature , with the help of the expansion valve-45, when the useful liquefied gas „y” 46 is produced, and, on the other hand, in the RB cycle, the He gas is sufering
• first a quasi-isothermal compression with multi-stage compressors 47 and stages provided each with TWRC and RRC-ULTR 48,
• then an adiabate expansion in a turbo-generator 49, and
• finally an isobar heating process in a heat exchanger 50, enabled by the subcooling of the fraction „y” of H 2 37 of the J-T cycle, in order to close tire cycle.
The procedure and achieving plant, according to invention, presented in example of Fig. 2, are capable to achieve, on one hand, for example, model operation parameters of H 2 liquefaction using the SCC- CBS-RB & J-T plant, noted as mentioned by H 2 -SCC-CBS-RB & J-T. The model output data are given in Fig. 3 and Fig. 4. Indeed, in Fig. 3 there are plotted the J-T expansion temperature, T 32 , the specific work Ispec and the useful liquefied gas fraction „y” 46, in function of the J-T expansion pressure, pzz. The results have been obtained considering the following main input data: i) sink source temperature, Tamb=288,15 K; ii) H 2 liquefaction temperature and pressiure, T 11-12 =20,4 K and p 11-12 =1 bar, respectively; iii) intermediary quasi-isothermal temperature of compression of the fraction „y” 34, T 13-31 =200,15 K, achieved by the compressors 35, RRC 36 and ULTR, means IHTF 32, at T D1 =198,15 K, in order to become the precooled fraction „y” 37, and iv) the Coefficient of Performance of the plant producing ULTR, described in Fig. 1, COP c , CBSthiswork =46 [kJ delivered cooling at T D1 =198, 15 K / kJ consumed mecanical work]. Out of Fig. 3, we remark that I spec decreases with the decrease of the parameters of J-T expansion, (T32; P32) for a Certain given COP c , CBSthiswork . The minimum value, = 1,728 [kWhe/kg liquid H 2 ] is much smaller as compared to that reported in the literature, e.g. l spec = 2,5. The figures of merit place l spec obtained in the ratio
(5,2 — 5,7)% as compared to the specific hydrogen burning power b H2 =
The procedure and achieving plant, according to invention, prezented in example of Fig. 2, are capable to solve in an efficient mode, on the other hand, the isobar He-H 2 heat exchange, which is critical in case of a conventional plant of H 2 liquefaction. Indeed, in Fig, 4 we plotted the thermal capability X[kJ * kg -1 K-1 ] of the fraction „y” of H 2 37, which enters the heat exchanger 38, noted by X H2 and that of He, which enters the heat exchanger 50, noted by X He . The plot has been done in the given example for H 2 inlet and outlet temperatures of the heat exchanger 38 for values T H2 ~ - while for He inlet and outlet temperatures of the heat exchanger 50, we used the values T He = The study case mentioned above is that having the most reduced specific mechanical work of liquefaction, = 1,728 [kWhe/kg liquid H2], for which the model considered that the J-T expansion pressure is p 32 = 4,85 bar, the H 2 si He mass flow rates have the values = 1kg /cycle and m He = 2, 3 kg /cycle, respectively, and the temperature pinch of the two fluids is 8T — 2K.
The achieving procedure, according to invention, describes in the example of Fig. 5 the evolution of the He gas which is intended to be liquefied, on one hand, in the J-T cycle, in several stages, namely,
• in the 1st stage, the subunit gas fraction „y”, e.g. y — 0.52, supplying externally the J-T cycle by the pressure and temperature sensibly equal to the ambient values and the mass equal to that to be liquefied, is precooled to a temperature value obtained by ULTR, • in the 2nd stage, the complementary gas fraction ,,1-y” of not liquefied gas, coming of the J-T expansion, and having the minimum pressure and temperature of liquefaction, e.g., p = 1bar,T ~ 4.3K, is sufering a first recovery heating process, subcooling the unit mass of gas, m = 1kg, which is obliged next to be J-T expanded and then is sufering a second recovery heating process till a temperature sensibly equal to that given by ULTR, e.g. T BI = 198.15K, subcooling a part of the gas found to the J-T expansion pressure,
• in the 3rd stage, fraction „y”, coming of the 1st stage, is mixing up with the gas fraction „1-y”, coming of the 2nd stage, in order to form a unit mass of gas, m =■ 1kg, of pressure and temperature sensible equal to that ofthe ambient and that resulting from ULTR, e.g. p = 1bar.T = 288.15K, respectively,
• in the 4th stage, the unit mass of gas, coming of the 3rd stage, is quasi-isothermal multi-stage compressed till the J-T expansion pressure, e.g, p = 8 bar, using external mechanical work input and TWR.C with RRC-ULTR in each stage,
• in the 5th stage, the unit mass of gas, coming of the 4th stage, is divided in two adequate complementary mass flow rates,
• in the 6th stage, the first gas complementary part, coming of the 5th stage, is recovery subcooled in the second recovejy heating process enabled by the complementary gas fraction ,,1-y", mentioned in the 2nd stage,
• in the 7th stage, the second complementary gas fraction coming of the 5th stage, is cooled in an isobar recovery heat exchange process in RB, e.g. T = 7.2K,
• in the 8th stage, the complementary gas fractions coming of the 5th stage are mixed up together after covering the 6th and 7th stages, in order to rebuild the unit mass of gas having the J-T expansion pessure and a temperature close to that resulting from the isobar recovery heat exchange process of RB, e.g. p = 8bar,T 7K,
• in the 9th stage, the unit mass of gas coming of the 8th stage, is subcooled finally in the first heat exchange process enabled by the recovery non liquefied complementary gas fraction ,,1-y" heating, mentioned in the 2nd stage and,
• in the 10th stage, the unit mass of gas coming from the 9th stage, found to the adequate J-T expansion pressure and temperature, e.g. p = 7bar,T = 5.9K, is expanded till the pressure and temperature of liquefaction, , e.g, p = 1bar, T = 4.3K, when the usefill liquefied gas fraction „y”, e.g. y=0.52, is produced, and, on the other hand, in the RB cycle, the He gas is sufering
• first a quasi-isothermal multi-stage compression done with external mechanical work input, e.g. w — 4154kJ/kg, and TWRC and RRC-ULTR use on each stage, from an adequate minimum pressure, e.g. p = 0.15bar, to a maximum pressure, e.g, p = 131.5bar,
•then an adiabatic expansion from the maximum pressure and a temperature sensible equal to that given by ULTR, e.g. T — 198.15K, till a minimum pressure and temperature, e,g. p = 0.15bar.T - 7.2K, when external mechanical work output is furnished, e.g. w = 946 kJ/kg, and
• then an isobar heating process of RB takes place from the minimum temperature, e.g. T = 7.2K, to a temperature sensibly equal to that given by ULTR, e.g. T - 198.15K, enabled by cooling of the complementary gas mass fraction of the unit mass of gas mentioned by Ute 7th stage, in order to close the cycle.
The applying plant, according to invention, given in the achievement example of Fig. 5, ensures on one hand, the evolution of the He gas to be liquefied in the J-T cycle, in several stages, namely
• in the 1st stage, a heat exchanger 51 is precooling the gas fraction „y” of gas 52 which must be liquefied, of ambient pressure, supplied externally, with the help of an ULTR plant, indicated by IHTF 32,
• in the 2nd stage, the gas fraction ,,1-y” 53, resulting from the J-T expansion, is sufering a first: recovery heating process in a heat exchanger 54, subcooling the unit mass of gas which is next J- T expanded and then a second recovery heating process in a second heat exchanger 55, subcooling a part of gas found to the J-T expansion pressure,
• in the 3rd stage, the subcooled gas fractions „y” 52 and ,,1-y” 53, coming of the first and second stage, respectively, are mixed up in order to rebuild the unit mass of gas 56 subcooled,
• in the 4th stage, the unit mass of gas 56 is compressed quasi-isothermal till the J-T expansion pressure, with the help of multi-stage compressors 57 and interstage TWRC with RRC-ULTR 58 done by ITHF 32,
• in the 5th stage, the unit mass of gas, coming of the 4th stage, is divided in two complementary gas fractions 59 and 60 with the help of a 3-way valve 61,
• in the 6th stage, the complementary gas fraction 59 is recoveiy subcooled by the second heating process of the complementary gas traction „1-y” 53, in the heat exchanger 55,
• in the 7th stage, the gas complementary fraction 60 is cooled in the recoveiy heat exchanger 62 of RB,
• in the 8th stage, the complementary gas fractions 59 and 60 are mixed up after being precooled, in order to form the unit mass of gas 63 with J-T expansion pressure and a temperature close to that resulting from the isobar recovery heat exchange process of RB,
• in the 9th stage, the unit mass of gas coming of the 8th stage, is subcooled finally in the heat exchanger 54, and
• in the 10th stage, the unit mass coming of the 9th stage, is J-T expanded from the pressure and temperature of expansion till the pressure and temperature of liquefaction. by the expansion valve 64, in order to produce the useful fraction of liquefied gas „y" 65, and on the other hand, in the RB cycle the He gas is sufering
• first a quasi-isothermal multi-stage compression 66, with TWRC and RRC-ULTR 67 means IHTF 32,
• then an adiabate expansion in a turbo-generator 68 till minimum pressure and temperature and
• finally an isobar heating process in the heat exchanger 69 enabled by the cooling of the complementary fraction 60, in order to close the cycle.
The procedure and achievement plant thereof according to invention, presented in the example of Fig. 5, are capable to achieve, on one hand, for example, model liquefaction parameters of He- SCC-CBS-RB & J-T plants in Fig. 6 si Fig. 7. Here we ploted the J-T expansion temperature, T32, the specific work. l spec and the useful fraction of liquefied gas „y” 65, in function of the J-T expansion pressure, p 32 . The results have been obtained considering the next main input data: i) sink sourse temperature, T am b=288,15 K; ii) He liquefaction temperature and pressure, T 11-12 =4,3 K and p 11-12 =1 bar, respectively; iii) the temperature of quasi-isothermal compression of the unit mass of gas 56, T 13-31 =200,15 K, achieved with tile compressors 53, RRC 58 and ULTR means IHTF 32 at T D1 =198,l 5 K, and iv) Coefficient of Performance of the ULTR plant, described in Fig. 1, COPc,cBsth»wk=46 [kJ delivered cooling at K / kJ consumed mecanical work].
Results show frat: a) in case of He, the T32 decrease by fractions of K degree, here by cca. 0,3 K, could decrease sigificantly the specific work Ispec and increase the useful fraction of liquefied gas „y” 65, for same J-T expansion pressure psz si COP c ,c8Sthisworfc; b) theoretically, it is possibe that Ispec be decreased to values enough reduced, e.g. here to l spec - 1,485, see Fig. 7, so that He be used as cryogenic agent in order to obtain superconductive materials with low critical temperatures, such as Niobium, with T c Nb-8,31 K, more economical and effective towards a clean energy future.
The achievement procedure, according to invention, schematically and generally describes in the example given in Fig. 8, the operation according to which the plant SCC-CBS-RB & J-T is selfinducing a supercoductibility state in its electrical driving devices structure, if these are build up of adequate materials, such as e.g. Nb in case of He liquefaction using a He -SCC-CBS-RB & J-T plant, or by e.g. NbjGc in case of H2 liquefaction obtained with the help of a H2-SCC-CBS-RB & J- T plant, and are cooled permanently to temperatures lower than the critical temperatures of the mentioned potential superconductive materils, i.e. up to T ≤ T CiNb = 8,31 K in case of Nb and up to T ≤ Tc.Nb^Ge — 22,4 K, in case of NbaGe, by using small amounts of the liquefied gas, in order to eliminate completely the irreversible dissipative electrical losses caused by the Joule effect occuring in the electrical conductors during plant operation.
The application plant, according to invention, given in the example of achievement of Fig. 8, is dividing the useful fraction of liquefied gas „y” 70, produced by SCC-CBS-RB & J-T, in two complementary mass flow rates, the first (1 - k~)y 71, used for external use and the second ky 72, used for selfinducing a superconductibility state in the electrical conductors of its own electrical conductors of the driving system, such as compressors, pumps, electrical consumers, where 0 < fc « 1, 0 < y < 1, ky « 1. The driving system is generically noted by 734, 73-2, ..., 73-(n-l), 73- n. The conductors of the driving system are made up of adequate materials which are cooled permanently by the fraction ky 72 with the help of the heat exchangers 74-1, 74-2, ..., 74-(n-l), 74- n, of a pump 75 pumping the fraction ky 72 and of a hydraulic circuit with two collectors 76 and pipes 77 connected in parallel between the two collectors 76, each provided with regulating valves 78. After cooling the electrical conductors, the liquid fraction ky 72 becomes the fraction of gas 79. This is joyning the complementary gas fraction (1 — k)y 80, introduced in the SCC-CBS-RB & J-T from the exterior in order to form the gas unit y 81 and to close the SCC-CBS-RB & J-T cycle with selfinduction of superconductibility of its electrical conductors.
The procedure and achieving plant thereof, according to invention, presented in the exmple of put in work order of Fig. 8, are capable to translate in practice, for example, model operating parameters of He liquefaction with He-SCC-CBS-RB & J-T and of H 2 with H 2 - SCC-CBS-RB & J-T, as those represented graphically in Fig. 9 and Fig. 10, respectively, for l sp,caisc [kWhe * kg -1 liquefied gas] va. LS-1V[m -1 ] where L[m] and S[m -2 ] are the length and section area of an electrical conductor, respectively. The input data of both figures have been calculated for two electrical current intensities in the conductors I max = 5 A and l max = 2A. The superconductors considered have been Nb, with T c ,Nb,He .=8,31 K, Fig. 9, and Nb 3 Ge, with T c,Nb3Ge = 22,4 K, Fig. 10. The input ambient temperature is T a -300 K, while the reference specific work considered was l spec 1.485 for LS -1 = 2,292e9 in case of Fig. 9 and l spec,H2 = 1,728 for LS -1 = l,783e9 in case of Fig. 10. From Fig. 9 and Fig. 10, we can remark that the use of the H 2 - and-He-SCC-CBS-RB & J-T benefiting additionally of selfinduction of superconductibility is capable to decrease considerably l spec as compared with the values obtained in Fig. 3 si Fig. 7 and with the other liquefaction technologies in kind. Moreover, if H 2 and He cryogenic fluids achievement could be done with low l spec in the future, as our results foresee, this gives great hope the low critical temperature superconductors may come in use again and replace those characterized by high critical temperatures, such as those based on ceramic cuprates materials, for instance, as being much cheaper arid feasible comparatively.
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